Simple Distillation Model

IntroductionThis spreadsheet is a simple distillation that cna be used to investigate the effect of design parameters on distillation performance. The calculation method uses a number of simplifying assumptions and should not beused in detailed design

The spreadsheet is split into the following sections

- A "How to Use This Calculation" Worksheet- The Distillation Worksheet itself - marked "Calculation" - A Theory Worksheet which presents the equations used in the calculation.

It is recommended that the user first reads the 'How to Use These Calculation' worksheet before starting a calculation.

RevisionRev. 1 Initial issue 22-Sep-11

held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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Disclaimer: This calculation provides a simplified model of a distillation column for preliminary design purposes only. We cannot be

Simple Distillation ModelRevision 1

See 'How to use these Calculation' worksheet for notes on its use. Cells in Green, with bold Text, to be completed by user - blue cells give calculated output

Calculation Title:

Press CRTL+Q to run model Type of Condenser

Condenser Partial CondenserRelative Volatility (Alpha) 2.4

DistillateTotal Molar Flowrate100.0 kmol/h

Mole fraction Benzene0.70

Mole fraction Toluene10 0.30

0.5FeedFeed Flow 100.0 kmol/hFeed Quality Vapour Feed

Feed TrayFeed Composition 6Component 1 ERROR MessagesBenzeneComponent 1 Mole Fraction0.70Component 2TolueneComponent 2 Mole Fraction0.30

Bottom Product Total Molar Flowrate

0.0 kmol/hMole fraction Benzene

0.00Mole fraction Toluene

1.00Condenser

responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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Total number of Trays Reflux Ratio

(Mole Basis)

Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held

Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

Simplified Distillation Model Revision 1

HOW TO USE THIS CALCULATION

1.0 INTRODUCTIONThis spreadsheet is a simplified model of a distilation which can be used to study the impact of design parameters on distillation performance. It is for use as a preliminary design tool only and should not be used to for the detailedspecification of a distillation column.

The simplified model is based on a number of key assumptions

1 It is a binary system - i.e. there are only two components in the mixture.

2 The two components are ideal, with a constant relative volatility. There is a constant molar overflow in the column as the two components have the same molar latent heat of evaporation and there are no heat losses or heat of mixing.

3 The plates are 100% efficient - each plate can be considered as one theoretical plate.

The assumptions underpinning the model are discussed in more detail in the Theory Worksheet.

2.0 How to use this spreadsheet

2.1 Colour CodingThe following colour coding is used:

Boxes shaded light green, with text in bold, require a user input.

Boxes shaded light blue give a calculated output. An error message is displayed if the user

attempts to overwrite the calculated value.

2.2 Calculation TitleThe spreadsheet leaves space to add a Calculation Title at the top. Although ths space is not strictly

necessary, it helps describe the calculation - this can be invaluable if it is to be checked by another

engineer.

2.3 Number of TraysThe user enters the total number of trays (or plates) in the column. It should be noted that each tray is assumed to 100% efficient (see theory worksheet for details). The column must have at least one tray and a maximum of ten.

2.4 Feed TrayThe user enters the position of the feed tray - i.e. the tray at which the feed enters the column. The traysare counted from the bottom. In other words Tray 1 is at the bottom just above the reboiler and Tray 2 isabove Tray 1. So if the column is specified with a total of 6 trays and the feed tray is number 3, the columnwill 3 trays below the feed tray, followed by the feed tray and then a further 2 trays above the feed tray.

The number of the feed tray cannot be greater than the total number of trays - the spreadsheet will display an error message if the user tries to do this.

2.5 Reflux RatioThe user must specify the Reflux Ratio on a molar basis. The Reflux Ratio is the liquid molar flow returning to the column divided by the distillate molar flow. As it is a fraction of the total distillate flow, it must have a value between zero and 1. If the reflux ratio is set to zero, there is no liquid returned to the top of thecolumn. This will mean that the section of the column above the feed does not achieve any separation. Separation is maximised by setting the reflux ratio to 1, however this means that no distillate product is collected. See the Theory Worksheet for more information.

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Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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2.6 Condenser TypeThe user must specify the type of condenser. There are two options: Full Condenser or Partial Condenser.If the Full Condenser option is selected, all of the vapour leaving the top tray is condensed. If the Partial Condenser option is selected, the distillate product is retrieved as a vapour while the condensate is returned to the column as a liquid. Hence, a partial condenser provides an additional separation stage. The differencies between the two options are discussed in more detail in the Theory Worksheet.

2.6 Feed Information - Component 1 and 2The user enters the names of components 1 and 2 (e.g. "Benzene" and "Toluene"). Like the calculation

title, this information is not strictly necessary, however it makes the output easier to follow.

2.7 Relative Volatility (Alpha)The user must input the relative volatility (alpha) of the two components. For an ideal mixture, the relative

volatility is the ratio of the two components' vapour pressures at a set temperature. For components with

similar boiling points, their relative volatility will be close to one, making them difficult to separate by

distillation. This can be studied using this spreadsheet by changing the value of alpha used.

The concept of relative volatility is discussed in more detail in the Theory Worksheet and is also discussed via the following link:

2.8 Feed FlowrateThe user enters the total molar flowrate, in kmol/h. This is the molar flow for both component 1 and 2.

2.9 Mole Fraction of Component 1The user inputs the mole fraction of Component 1 in the Feed. This must be a value between 0 and 1. Asthis is a binary system, the spreadsheet automatically calculates the mole fraction of Component 2 in the feed.

2.10 Feed QualityThe user inputs the feed quality. There are three options: "Liquid Feed", "Vapour Feed" or "Mixed Feed". If "Liquid Feed" is selected, the feed is treated as a saturated liquid. If "Vapour Feed" is selected, the feed is treated as a saturated vapour. If "Mixed Feed" is selected, the feed is treated as 50% liquid and 50% vapour. Sub-cooled liquid feed or superheated vapour feeds are not possible.

2.11 Distillate FlowrateThe user enters the Distillate (Top) Product total molar flowrate, in kmol/h. This is the molar flow for both

component 1 and 2.

2.12 Distillate Mole FractionsThe spreadsheet will calculate the component mole fractions in the distillate. This requires the use of amacro (see "Solving the Spreadsheet" below). If the spreadsheet has not converged, no mole fractions will be displaced.

2.13 Bottom Product Flowrate and Mole FractionsThe spreadsheet calculates both the total bottom product flow rate and mole fractions. As with the distillatemole fractions, these require the use of a macro (Press CTRL+Q) to solve, If the spreadsheet has notconverged, no mole fractions will be displaced.

3.0 SOLVING THE SPREADSHEETAs noted above, the spreadsheet uses a macro to calculate the distillate and bottom product compositions.Therefore, to make this spreadsheet work, macros must not be disabled. The macro is activated by pressing the keys CTRL and Q simultaneously.

Relative Volatility

Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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4.0 ERROR MESSAGESThe spreadsheet can display a number of error messages.

Many of the input cells are limited to certain values. For example, the component mole fractions must bebetween 0 and 1. If the user attempts to input a value outside the acceptable range, the spreadsheet willalert the user.

When the user first inputs values into the spreadsheet, an error message will be displayed that the calculation has not converged. To converge the calculation, activate the macro (CTRL+Q).

The spreadsheet will also alert the user if parts of the column have a vapour or liquid flow below zero. If this occurs, the user should adjust one, or more, of the following: feed quality, reflux ratio, distillate molarflowrate.

Finally, the spreadsheet will warn the user if the Distillate flow is greater than the Feed flow - a situationwhich is clearly not feasible.

Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

Simplified Distillation Model Revision 1

CALCULATION THEORY

1.0 INTRODUCTIONThis spreadsheet is a simplified model of a distilation which can be used to study the impact of design parameters on distillation performance. It is for use as a preliminary design tool only and should not be used to for the detailedspecification of a distillation column.

2.0 ASSUMPTIONS USED IN THE MODELTo keep the model simple, a number of simplifications are made:

Binary SystemThe number of equations required to solve a distillation model increases dramatically as the number of componentsincreases. Therefore, to minimise complexity, the model is based on a binary system (i.e. Only two components).

Heat BalanceTo reduce the number of equations still further, the heat balance is ignored. This means that the model does not predict operating temperatures in the column. To allow the heat balance to be ignored, the following assumptions are made to the model:

i. The latent heat of vaporisation for both components is the same. As a consequence, the vapour and liquidflows in both the rectifying and stripping sections of the column remain constant.

ii. The feed flow is assumed to be at its boiling point - either saturated vapour, saturated liquid or a mix ofvapour and liquid. Sub-cooled liquid or superheated vapour feeds are not permitted.

iii There are no heat losses from the distillation column.

Vapour / Liquid EquilibriumA simplified physical property model is used to calculate vapour-liquid equilibrium. The model assumes that the system has a constant relative volatility.

Stage EfficiencyLiquid entrainment in the vapour, weepage of liquid through the vapour perforations in the plate, as well as other

imperfections, mean that plates in real distillation columns are not 100% efficient. These effects are ignored in themodel.

3.0 CALCULATION OF THE OVERALL MASS BALANCEThe overall column mass balance is calculated by the model by splitting the column into two parts:

i. The Rectifying (Top) Section of the Distillation Column - this is the part of the distillation column above the

feed plate, including the condenser.

ii. The Enriching (Bottom) Section of the Distillation Column - this is the part of the distillation column below

the feed plate, including the reboiler.

3.1 Overall Mass Balance on the Rectifying Section

A sketch of the Rectifying Section is shown in Figure 1 below:

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Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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The reflux flow sets the liquid flow down the Rectifying Section of the Column.

Where:

Reflux Flow - Reflux molar flow returning to the column from the condenser, kmol/h

L_Rectifying - Liquid molar flow down the Rectifying Section of the Column, kmol/h

D - Distillate molar flow leaving the column as product, kmol/h

R - Molar Reflux Ratio (Dimensionless)

The vapour flow up the Rectifying Section of the column is set by the vapour flow up the stripping section plus the

vapour fraction of the feed flow into the column.

Where:

V_Rectifying - Vapour molar flow down the Rectifying Section of the Column, kmol/h

F - Feed molar flow into the Column, kmol/h

Quality - Feed Quality (Dimensionless)

V_Stripping - Vapour molar flow down the Stripping Section of the Column, kmol/h

The feed quality is set by the user when they define the feed. If a liquid feed is specified, there is no feed

contribution to the vapour flow in the rectifying section of the column (Quality = 1). If a vapour feed is specified,

all the feed flows up the rectifying section (Quality =0). If a mixed feed is specified, half of the feed flows up the

rectifying section of the column (Quality = 0.5).

3.2 Overall Mass Balance on the Stripping SectionA sketch of the Stripping Section is shown in Figure 2 below:

Reflux Flow = L_Rectifying = D x R Equation (1)

V_Rectifying = F x (1 - Quality) + V_Stripping Equation (2)

Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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As the Feed flow and Distillate flow is set by the user, the Bottom product flow, B, (in kmol/h) can be calculated:

The liquid flow up the Stripping Section of the column is set by the liquid flow down the rectifying section plus the

liquid fraction of the feed flow into the column.

Where:

L_Stripping - Liquid molar flow down the Stripping Section of the Column, kmol/h

The vapour flow up the distillation column is the quantity of vapour generated by the reboiler. In the mass balance

it is the difference between the liquid flow down the stripping section and the bottom product.

3.3 Component Molar BalanceHaving established the overall vapour and liquid flows within the column, the spreadsheet performs a tray

by tray component molar balance. This is an iterative calculation - hence the need for a macro. As there areonly two components, calculating the mole fraction of one component fixes the other. The following approach isfollowed for each stage

B = F - D Equation (3)

L_Stripping = F x Quality + L_Rectifying Equation (4)

V_Stripping = L_Stripping - B Equation (5)

Disclaimer: This calculation is a simplified model of a distillation column for preliminary design. We cannot be held responsible for its use. As with all areas of process engineering, calculations should be checked by a competent engineer.

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1. Guess the liquid mole fraction, x, of component 1

2. Calculate the vapour mole fraction, y, of component 2, using relatively volatility - see Equation 6.

3. Perform a molar balance for component 1 over each the stage. This is a calculation of the molar flow entering and leaving the stage. For the feed tray, the molar balance considers the component feed flowonto the tray.

4 If the molar flows onto and off the tray do not balance, the macro re-adjusts the tray liquid mole fraction.The model is solved when the mole fractions on each stage is balanced.

y = a.x

[1+( -1).a x] Equation (6)